NO150078B - PROCEDURE FOR THE EXTRACTION OF SURE ALKYLATES CREATED BY THE ALKYLATION OF AROMATIC HYDROCARBONES IN THE PRESENT OF ALUMINUM CHLORIDE - Google Patents

PROCEDURE FOR THE EXTRACTION OF SURE ALKYLATES CREATED BY THE ALKYLATION OF AROMATIC HYDROCARBONES IN THE PRESENT OF ALUMINUM CHLORIDE Download PDF

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Publication number
NO150078B
NO150078B NO763847A NO763847A NO150078B NO 150078 B NO150078 B NO 150078B NO 763847 A NO763847 A NO 763847A NO 763847 A NO763847 A NO 763847A NO 150078 B NO150078 B NO 150078B
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Prior art keywords
alkylates
aluminum chloride
alkylation
salts
ammonia
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NO763847A
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Norwegian (no)
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NO763847L (en
NO150078C (en
Inventor
Philippe Jean Gillet
Gaston Henrich
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Charbonnages Ste Chimique
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Filing date
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Priority claimed from FR7534704A external-priority patent/FR2331379A1/en
Priority claimed from FR7534703A external-priority patent/FR2331537A1/en
Application filed by Charbonnages Ste Chimique filed Critical Charbonnages Ste Chimique
Publication of NO763847L publication Critical patent/NO763847L/no
Publication of NO150078B publication Critical patent/NO150078B/en
Publication of NO150078C publication Critical patent/NO150078C/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/009—Heating or cooling mechanisms specially adapted for settling tanks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/28—Regeneration or reactivation
    • B01J27/32—Regeneration or reactivation of catalysts comprising compounds of halogens
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F7/00—Compounds of aluminium
    • C01F7/48—Halides, with or without other cations besides aluminium
    • C01F7/56—Chlorides
    • C01F7/62—Purification
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
    • C07C2/66—Catalytic processes
    • C07C2/68—Catalytic processes with halides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/06—Halogens; Compounds thereof
    • C07C2527/08—Halides
    • C07C2527/10—Chlorides
    • C07C2527/11—Hydrogen chloride
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/06—Halogens; Compounds thereof
    • C07C2527/125—Compounds comprising a halogen and scandium, yttrium, aluminium, gallium, indium or thallium
    • C07C2527/126—Aluminium chloride
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Description

Den foreliggende oppfinnelse angår en fremgangsmåte til utvinning av sure alkylater dannet ved alkylering av aromatiske hydrokarboner i nærvær av aluminumklorid, hvor alkylatene nøy-traliseres med vannfri ammoniakk i et første trinn, hvorved det dannes saltkomplekser av aluminiumklorid og ammoniakk, karakterisert ved at man i et ytterligere trinn underkaster saltkompleksene en flokkulering ved tilsetning av vanndamp, i en mengde som tilsvarer fra 10 til 20 vektprosent av tørrvekten av de flokkuierte salter, og deretter skiller alkylatene fra de flokkulerte salter. The present invention relates to a method for extracting acidic alkylates formed by alkylation of aromatic hydrocarbons in the presence of aluminum chloride, where the alkylates are neutralized with anhydrous ammonia in a first step, whereby salt complexes of aluminum chloride and ammonia are formed, characterized in that in a a further step subjects the salt complexes to flocculation by adding steam, in an amount corresponding to from 10 to 20% by weight of the dry weight of the flocculated salts, and then separates the alkylates from the flocculated salts.

Som kjent anvendes Friedel-Crafts-reaksjonen industrielt, spesielt ved fremstilling av etylbenzen fra etylen og benzen, As is known, the Friedel-Crafts reaction is used industrially, especially in the production of ethylbenzene from ethylene and benzene,

av kumen fra propylen og benzen, samt kymener fra toluen og propylen. Etter alkylering erholdes ved sedimentering/klaring på den ene side alkylater inneholdende en viss mengde oppløst katalytisk kompleks og på den annen side et katalytisk kompleks kjent som "rød olje", hvorav en tredjedel er mineralske materi-aler (aluminiumsalter, HC1), og to tredjedeler er hydrokarboner. Alkylatene behandles vanligvis med en base, såsom soda eller ammoniakk, og deretter med vann og så igjen - om det ønskes - med soda, hvilket har den ulempe at alkylater fjernes med vas-keløsningene, hvilket medfører tap og eventuelt forurensning av de elver eller lignende som mottar avfallet. of cumene from propylene and benzene, as well as cymenes from toluene and propylene. After alkylation, sedimentation/clarification yields, on the one hand, alkylates containing a certain amount of dissolved catalytic complex and, on the other hand, a catalytic complex known as "red oil", one third of which is mineral materials (aluminium salts, HC1), and two thirds are hydrocarbons. The alkylates are usually treated with a base, such as soda ash or ammonia, and then with water and then again - if desired - with soda ash, which has the disadvantage that alkylates are removed with the washing solutions, which entails loss and possible pollution of the rivers or the like which receives the waste.

I den senere tid er det blitt oppdaget at det er mulig å nøytralisere de sure alkylater, etter separasjon fra komplekset, med vannfri ammoniakk, fortrinnsvis i gassform, hvorved forurensning av elver etc. og tap av alkylater unngås. In recent times, it has been discovered that it is possible to neutralize the acidic alkylates, after separation from the complex, with anhydrous ammonia, preferably in gaseous form, whereby pollution of rivers etc. and loss of alkylates is avoided.

Etter denne behandling erholdes i suspensjon i alkylatet After this treatment is obtained in suspension in the alkylate

en blanding av salter bestående av aluminiumklorid og et kompleks som dannes når ammoniakk reagerer med AlCl^. a mixture of salts consisting of aluminum chloride and a complex formed when ammonia reacts with AlCl^.

Separasjonen av blandingen av salter som erholdes kan skje ved sedimentering, men den tid som er påkrevet for oppnåelse av tilstrekkelig klaring, er lang, av størrelsesorden 36 - 80 ti-mer, og representerer en prohibitiv kostnad i praksis. Sentrifugering gir hurtigere resultater, men krever bruk av meget store installasjoner når man ønsker å behandle store mengder av alkylater, og det erholdte resultat er ofte utilfredsstillende. Med hensyn til filtrering, så er også denne kostbar og vanskelig å anvende når det dreier seg om behandling av de meget store mengder som erholdes i moderne anlegg for syntese av etylbenzen ved fremstilling av styren eller kumen for fremstilling av fe-nol. The separation of the mixture of salts that is obtained can take place by sedimentation, but the time required to achieve sufficient clarification is long, of the order of 36 - 80 hours, and represents a prohibitive cost in practice. Centrifugation gives faster results, but requires the use of very large installations when you want to process large quantities of alkylates, and the results obtained are often unsatisfactory. With regard to filtration, this is also expensive and difficult to use when it comes to treating the very large quantities obtained in modern plants for the synthesis of ethylbenzene in the production of styrene or cumene for the production of phenol.

Det ble nå oppdaget at det er mulig å oppnå hurtig og fullstendig klaring ved tilsetning av en liten mengde vanndamp. It was now discovered that it is possible to achieve rapid and complete clarification by adding a small amount of steam.

Ved fremgangsmåten ifølge oppfinnelsen oppnås flokkulering av saltene i et alkylat som er nøytralisert med vannfri ammoniakk, idet vanndampen tilsettes under omrøring, hvoretter man lar saltene synke til den nedre del av apparatet (bunnen); mengden av vanndamp som tilsettes representerer fortrinnsvis 15-20 vektprosent, beregnet på de tørre salter. In the method according to the invention, flocculation of the salts is achieved in an alkylate which has been neutralized with anhydrous ammonia, the water vapor being added while stirring, after which the salts are allowed to sink to the lower part of the apparatus (bottom); the amount of water vapor that is added preferably represents 15-20 percent by weight, calculated on the dry salts.

I henhold til en foretrukken utførelsesform av oppfinnelsen tilsettes vanndampen i form av en blanding av vanndamp og inert gass, fortrinnsvis nitrogen, hvilket også medfører en ønsket omrøring av innholdet i flokkuleringsapparatet. Andelen av vanndamp og av nitrogen beregnes fortrinnsvis slik at det ikke erholdes fritt kondensert vann i apparatet. Den avhenger således av temperaturen i dette. Med sikte på anvendelse av minimal nitrogentilførsel kan det være hensiktsmessig å anvende temperaturer på eksempelvis omkring 50°C. According to a preferred embodiment of the invention, the water vapor is added in the form of a mixture of water vapor and inert gas, preferably nitrogen, which also results in the desired stirring of the contents of the flocculation apparatus. The proportion of water vapor and nitrogen is preferably calculated so that no free condensed water is obtained in the apparatus. It thus depends on the temperature in this. With a view to using a minimal nitrogen supply, it may be appropriate to use temperatures of, for example, around 50°C.

Under disse betingelser flokkuleres saltene på en bemerkel-sesverdig måte, og de således erholdte salter lar seg lett fra-skille . Under these conditions, the salts flocculate in a remarkable manner, and the salts thus obtained can be easily separated.

Etter klaring erholdes i bunnen av beholderen et saltrikt produkt som kan behandles ved sentrifugering og deretter filtrering, mens materialet i den øvre del av beholderen ikke inneholder salter. After clarification, a salt-rich product is obtained at the bottom of the container which can be processed by centrifugation and then filtration, while the material in the upper part of the container does not contain salts.

Fremgangsmåten ifølge oppfinnelsen kan anvendes i forbindelse med alle alkyleringsprosesser hvor det anvendes aluminiumklorid og hvor alkylatenes art tillater behandling med ammoniakk. Den kan anvendes på alkylater som er nøytralisert med vannfri ammoniakk, og i forbindelse med blandinger av alkylater og kata-lysatorrester, og spesielt katalytiske komplekser fra alkyle-ringsreaksjoner i nærvær av aluminiumklorid (rød olje) i suspensjon i et aromatisk hydrokarbonmedium. The method according to the invention can be used in connection with all alkylation processes where aluminum chloride is used and where the nature of the alkylates allows treatment with ammonia. It can be used on alkylates that have been neutralized with anhydrous ammonia, and in connection with mixtures of alkylates and catalyst residues, and especially catalytic complexes from alkylation reactions in the presence of aluminum chloride (red oil) in suspension in an aromatic hydrocarbon medium.

Det ble faktisk oppdaget at disse oljer kunne nøytralise-res ved at de intensivt dispergeres i ett eller flere aromatiske hydrokarboner og nøytraliseres med gassformig ammoniakk under kraftig omrøring. It was actually discovered that these oils could be neutralized by intensively dispersing them in one or more aromatic hydrocarbons and neutralizing them with gaseous ammonia under vigorous stirring.

De følgende eksempler vil ytterligere belyse oppfinnelsen. The following examples will further illustrate the invention.

EKSEMPEL 1 EXAMPLE 1

Nøytralisering av det katalytiske kompleks Neutralization of the catalytic complex

Alkylatet erholdes fra en reaktor for fremstilling av etylbenzen, hvor benzen alkyleres med etylen i nærvær av aluminiumklorid og etylklorid som aktivator. The alkylate is obtained from a reactor for the production of ethylbenzene, where benzene is alkylated with ethylene in the presence of aluminum chloride and ethyl chloride as activator.

Ved alkyleringsreaktorens utløp erholdes 50 l/time surt alkylat inneholdende 60 ml oppløst kompleks, samt en oljeaktig kompleksfase hvorav det utblåses 100 ml/time, idet resten resirkuleres til alkyleringsreaktoren. Blandingen av alkylat og utblåst kompleks behandles i en rør-nøytralisator med diameter på 5 cm og høyde på 100 cm, hvor blandingen sirkuleres ved hjelp av en pumpe med en kapasitet på 300 l/time. Blandingen av kompleks og alkylat tilføres i høyde med pumpen. Ved bunnen av nøytralisatoren til-føres 200 normal-liter ammoniakk pr. time f overskuddet av ammoniakk samles i den øvre del av nøytralisatoren, og alkylatet avdestilleres for utvinning av etylbenzenet. At the outlet of the alkylation reactor, 50 l/hour of acid alkylate containing 60 ml of dissolved complex is obtained, as well as an oily complex phase of which 100 ml/hour is blown off, the rest being recycled to the alkylation reactor. The mixture of alkylate and blown complex is treated in a pipe neutralizer with a diameter of 5 cm and a height of 100 cm, where the mixture is circulated by means of a pump with a capacity of 300 l/hour. The mixture of complex and alkylate is supplied at the height of the pump. At the bottom of the neutralizer, 200 normal liters of ammonia are added per hour f the excess of ammonia is collected in the upper part of the neutralizer, and the alkylate is distilled off to recover the ethylbenzene.

Under disse betingelser spaltes katalysatoren fullstendig i ammoniumklorid og et salt som dannes av AlCl^ og NH^. Driften er pålitelig, og ingen avsetninger observeres på reaktorveggene selv etter flere måneders kontinuerlig drift. Under these conditions, the catalyst is completely decomposed into ammonium chloride and a salt formed from AlCl^ and NH^. The operation is reliable, and no deposits are observed on the reactor walls even after several months of continuous operation.

EKSEMPEL 2 EXAMPLE 2

Dette eksempel viser at det er mulig å arbeide med større strømningshastigheter og langt høyere konsentrasjoner av komplekser. This example shows that it is possible to work with greater flow rates and much higher concentrations of complexes.

Fremgangsmåten er som i eksempel 1, og det anvendes The procedure is as in example 1, and it is used

samme nøytralisator og samme sirkulasjonspumpe. Strømningshastig-hetene er som følger: same neutralizer and same circulation pump. The flow rates are as follows:

- Tilførsel av alkylater: 50 l/time inneholdende 60 cm<3> av - Supply of alkylates: 50 l/hour containing 60 cm<3> of

oppløst kompleks dissolved complex

- Tilførsel av fritt - Supply of free

kompleks: 2,5 l/time complex: 2.5 l/hour

- Tilførsel av ammoniakk: 2 000 l/time. - Supply of ammonia: 2,000 l/hour.

De samme resultater erholdes som i det foregående eksempel. The same results are obtained as in the previous example.

EKSEMPEL 3 EXAMPLE 3

Separasjon av saltene Separation of the salts

Fremgangsmåten er som i eksempel 1. 4 0 kg/time av det nøytraliserte alkylat tilføres et flokkuleringsapparat bestående av en rørreaktor med diameter på 5 cm og høyde på 6 0 cm. The procedure is as in example 1. 40 kg/hour of the neutralized alkylate is supplied to a flocculation apparatus consisting of a tube reactor with a diameter of 5 cm and a height of 60 cm.

.Alkylatet 0,5 vektprosent salter. .The alkylate 0.5% by weight salts.

I apparatets nedre del tilføres 200 normal-liter pr.N:ime oppvarmet nitrogen inneholdende vanndamp tilsvarende 35 g/time. Nitrogenstrømmens temperatur er slik at apparatet holdes ved en temperatur mellom 50 og 6 0°C. In the lower part of the device, 200 normal liters per hour of heated nitrogen containing water vapor corresponding to 35 g/hour are supplied. The temperature of the nitrogen flow is such that the apparatus is kept at a temperature between 50 and 60°C.

Det således behandlede alkylat føres inn i en klaringstank. I bunnen av denne tank erholdes en væske i hvilken de flokkulerte salter er fem ganger mer konsentrert enn i det opprinne-lige alkylat. Denne blanding behandles i en kontinuerlig arbei-dende sentrifuge. Ved sentrifugens utløp erholdes et renset alkylat inneholdende høyst noen titall ppm salter; dessuten erholdes et slam. Dette slam tørres, og man gjenvinner for det første ammoniakk, som resirkuleres til nøytralisatoren, og for det andre hydrokarboner, som likeledes resirkuleres. The thus treated alkylate is fed into a clarification tank. At the bottom of this tank, a liquid is obtained in which the flocculated salts are five times more concentrated than in the original alkylate. This mixture is processed in a continuously operating centrifuge. At the outlet of the centrifuge, a purified alkylate containing at most a few tens of ppm of salts is obtained; moreover, a sludge is obtained. This sludge is dried, and one recovers, firstly, ammonia, which is recycled to the neutralizer, and secondly, hydrocarbons, which are likewise recycled.

Det klarede alkylat som uttas fra den øvre del av klaringstanken, inneholder ikke salter og blandes med det rensede alkylat og blir så filtrert og til slutt avgasset i en kolonne med totalt tilbakeløp. Ammoniakken resirkuleres til nøytralisatoren. The clarified alkylate which is withdrawn from the upper part of the clarification tank does not contain salts and is mixed with the purified alkylate and is then filtered and finally degassed in a column with total reflux. The ammonia is recycled to the neutralizer.

Det er imidlertid også mulig å sløyfe filtreringen av det alkylat som uttas fra den øvre del av klaringstanken, idet bare det nevnte, ved sentrifugering rensede alkylat filtreres, eller endog å eliminere filteret helt. However, it is also possible to skip the filtration of the alkylate which is removed from the upper part of the clarification tank, as only the aforementioned alkylate purified by centrifugation is filtered, or even to eliminate the filter altogether.

Claims (3)

1 . Fremgangsmåte til utvinning av sure alkylater dannet ved alkylering av aromatiske hydrokarboner i nærvær av aluminiumklorid, hvor alkylatene nøytraliseres med vannfri ammoniakk i et første trinn, hvorved det dannes saltkomplekser av aluminiumklorid og ammoniakk, karakterisert ved at man i et ytterligere trinn underkaster saltkompleksene en flokkulering ved tilsetning av vanndamp, i en mengde som tilsvarer fra 1 0 til 20 vektprosent av tørrvekten av de flokkulerte salter, og deretter skiller alkylatene fra de flokkulerte salter.1. Process for the recovery of acidic alkylates formed by alkylation of aromatic hydrocarbons in the presence of aluminum chloride, where the alkylates are neutralized with anhydrous ammonia in a first step, whereby salt complexes of aluminum chloride and ammonia are formed, characterized in that, in a further step, the salt complexes are subjected to flocculation by the addition of steam, in an amount corresponding to from 10 to 20 percent by weight of the dry weight of the flocculated salts, and then the alkylates are separated from the flocculated salts. 2. Fremgangsmåte ifølge krav 1, karakterisert ved at man anvender en inert gasstrøm, fortrinnsvis nitrogen, for innføringen av vanndampen i flokkuleringsapparatet.2. Method according to claim 1, characterized by using an inert gas flow, preferably nitrogen, for introducing the water vapor into the flocculation apparatus. 3. Fremgangsmåte ifølge et av de foregående krav, karakterisert ved at flokkuleringsapparatet holdes ved en temperatur som er tilstrekkelig til å hindre kon-densasjon av fritt vann.3. Method according to one of the preceding claims, characterized in that the flocculation apparatus is kept at a temperature which is sufficient to prevent condensation of free water.
NO763847A 1975-11-13 1976-11-11 PROCEDURE FOR THE EXTRACTION OF SURE ALKYLATES CREATED BY THE ALKYLATION OF AROMATIC HYDROCARBONES IN THE PRESENT OF ALUMINUM CHLORIDE NO150078C (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7534704A FR2331379A1 (en) 1975-11-13 1975-11-13 Separating salts from alkylate neutralisation with ammonia - in Friedel:Crafts reaction, after flocculating with water
FR7534703A FR2331537A1 (en) 1975-11-13 1975-11-13 Neutralisation of Friedel-Crafts alkylation catalysts - with gaseous ammonia in aromatic hydrocarbon medium (BR 10.5.77)

Publications (3)

Publication Number Publication Date
NO763847L NO763847L (en) 1977-05-16
NO150078B true NO150078B (en) 1984-05-07
NO150078C NO150078C (en) 1984-08-22

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US (1) US4117023A (en)
DE (1) DE2651698C2 (en)
DK (1) DK155593C (en)
FI (1) FI61681C (en)
MX (1) MX4893E (en)
NO (1) NO150078C (en)
PT (1) PT65786B (en)
SE (1) SE428013B (en)
SU (1) SU955854A3 (en)

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JPS59157035A (en) * 1983-02-28 1984-09-06 Kyowa Chem Ind Co Ltd Removal of halogen component from organic compound containing halogen-containing catalyst
FR2566770B1 (en) * 1984-06-27 1986-11-14 Inst Francais Du Petrole IMPROVED PROCESS FOR REMOVING NICKEL, ALUMINUM AND CHLORINE FROM OLEFIN OLIGOMERS
US4940833A (en) * 1988-11-29 1990-07-10 Phillips Petroleum Company Olefin monomer separation process
US5743298A (en) * 1996-04-22 1998-04-28 Techniflo Corporation Spring pulsation dampener
US5996632A (en) * 1998-12-14 1999-12-07 Aeroquip Corporation Pressure relief adapter
US20080033227A1 (en) * 2006-08-03 2008-02-07 David Campbell Graves Recovery of sulfur value in an alkylation process
CN110078691A (en) * 2019-05-05 2019-08-02 山东盛华新材料科技股份有限公司 The recovery method of catalyst in a kind of heterocyclic Friedel-Crafts reaction

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US2376088A (en) * 1939-10-04 1945-05-15 Dow Chemcial Company Method of treating friedel-crafts reaction liquors
US3499054A (en) * 1968-08-19 1970-03-03 Continental Oil Co Purification of detergent alkylates
US3679770A (en) * 1970-08-10 1972-07-25 Standard Oil Co Process for removal of catalyst complex
US3703559A (en) * 1970-11-25 1972-11-21 Continental Oil Co Purification of detergent alkylates

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DE2651698C2 (en) 1983-10-13
SE428013B (en) 1983-05-30
SE7612113L (en) 1977-05-14
SU955854A3 (en) 1982-08-30
FI61681B (en) 1982-05-31
DK155593B (en) 1989-04-24
DE2651698A1 (en) 1977-06-02
DK155593C (en) 1989-09-18
PT65786B (en) 1978-05-10
NO763847L (en) 1977-05-16
FI763222A (en) 1977-05-14
US4117023A (en) 1978-09-26
DK511776A (en) 1977-05-14
PT65786A (en) 1976-12-01
MX4893E (en) 1982-12-09
NO150078C (en) 1984-08-22
FI61681C (en) 1982-09-10

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